CN102811982A - Process and apparatus for increasing weight of olefins - Google Patents
Process and apparatus for increasing weight of olefins Download PDFInfo
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- CN102811982A CN102811982A CN2011800150770A CN201180015077A CN102811982A CN 102811982 A CN102811982 A CN 102811982A CN 2011800150770 A CN2011800150770 A CN 2011800150770A CN 201180015077 A CN201180015077 A CN 201180015077A CN 102811982 A CN102811982 A CN 102811982A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C15/00—Cyclic hydrocarbons containing only six-membered aromatic rings as cyclic parts
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/14858—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound with inorganic compounds not provided for before
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
- C07C7/177—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by selective oligomerisation or polymerisation of at least one compound of the mixture
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
- C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
- C10G29/20—Organic compounds not containing metal atoms
- C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
- C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
- C10G55/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G57/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process
- C10G57/005—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one cracking process or refining process and at least one other conversion process with alkylation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1081—Alkanes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1088—Olefins
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1096—Aromatics or polyaromatics
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/28—Propane and butane
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The process and apparatus converts FCC olefins to heavier compounds. The heavier compounds are more easily separated from the unconverted paraffins. The heavier compounds can be recycled to an FCC unit or delivered to a separate FCC unit. Suitable conversion zones are oligomerization and aromatic alkylation zones.
Description
The priority request of national applications early
The application requires the U. S. application Nos.12/751 of submission on March 31st, 2010,623 and 12/751,658 right of priority.
Background of invention
Invention field of the present invention is to be used for become higher molecular weight compound with easy and the isolating method and apparatus of unconverted paraffinic hydrocarbons with paraffinic hydrocarbons blended conversion of olefines.
Fluid catalystic cracking (FCC) is for contacting the catalytic hydrocarbon method for transformation of realizing through making than heavy hydrocarbon with the catalysed particulate material in fluidized bed reaction zone.Compare with hydrogen cracking, being reflected in the catalytic cracking do not exist under hydrogen or the hydrogen consumption of a large amount of addings carries out.When cracking reaction was carried out, a large amount of high carbonaceous materials that is called coke was deposited on the catalyzer so that pyrogenic catalyzer or spent catalyst to be provided.The light product of gaseous state separates with spent catalyst in reaction vessel.The carbonaceous gas that the stripping that can make spent catalyst stand rare gas element such as steam goes out to carry secretly with stripping from spent catalyst.In the breeding blanket with the high temperature regeneration of oxygen with coke from burning the steam stripped spent catalyst.Various products can be produced by this method, comprise naphtha products and/or lighter products such as propylene and/or ethene.
In these class methods, can use single reactor or double-reactor.Although use double-reactor equipment possibly cause extra cost of capital, can operate a reactor drum with condition of compatibility so that product such as light olefin comprise the maximization of propylene and/or ethene.
Usually advantageously can make a product yield maximization in the reactor drum.In addition, possibly hope to make the product maximize production of a reactor drum, but said product recycling is returned in another reactor drum to produce required product such as propylene.C
4-C
7
C
4-C
7The cracking of alkene produces high propylene yield.Rich C C
4-C
7Materials flow recycling is returned and can be used for further improving propone output in the FCC reactor drum.Yet this recycling causes in the recycle stream the more enrichment of refractory paraffinic hydrocarbons and requires significant the cleaning or big recycling flow velocity.As far as having the materials flow of this wide region boiling point, do not exist alkene and the isolating simple method of paraffinic hydrocarbons.
Alkene heavier alkene of oligomeric one-tenth under the heterogeneous catalyst effect is known technology with the preparation motor spirit.Also known under homogeneous acid catalyst with paraffinic hydrocarbons with olefin alkylation with the preparation motor spirit.Also known usually under the heterogeneous catalyst effect with benzene and other aromatic component alkylation with the preparation petrochemical materials, comprise the purification agent precursor.
Need easily the alkene in the product stream to be separated with paraffinic hydrocarbons.
Summary of the invention
In exemplary, the present invention relates to conversion of olefines is become the more method of large compound.Make C
4Alkene and paraffinic hydrocarbons and C
5-C
7Alkene and paraffinic hydrocarbons get in the zone of transformation to pass through with aromatic hydrocarbons C
5-C
7Olefin alkylation and with C
4Conversion of olefines becomes more macromolecule C
4Derivative compound and with C
5-C
7Conversion of olefines becomes more macromolecule C
5-C
7Derivative compound.With C
4Derivative compound and C
4Alkene separates with paraffinic hydrocarbons, and with C
5-C
7Derivative compound and C
5-C
7Alkene separates with paraffinic hydrocarbons.At last, with C
4Derivative compound and C
5-C
7Derivative compound infeeds in the FCC reactor drum.
In another exemplary, the present invention relates to conversion of olefines is become the more method of large compound.Make C
5-C
7First materials flow of alkene and paraffinic hydrocarbons gets in first zone of transformation with C
5-C
7Conversion of olefines becomes more macromolecule C
5-C
7Derivative compound.Make C
4Second materials flow of alkene and paraffinic hydrocarbons gets in second zone of transformation with C
4Conversion of olefines becomes more macromolecule C
4Derivative compound.With C
4Derivative compound and C
4Alkene separates with paraffinic hydrocarbons, and with C
5-C
7Derivative compound and C
5-C
7Alkene separates with paraffinic hydrocarbons.At last, with C
4Derivative compound and C
5-C
7Derivative compound infeeds in the FCC reactor drum.
In another exemplary, the present invention relates to conversion of olefines is become the more method of large compound.Make cracking catalyst contact with the hydrocarbon incoming flow with hydrocarbon cracking is become to have the crackate hydrocarbon of lower molecular weight and make sedimentation of coke on cracking catalyst so that the coking cracking catalyst to be provided.The coking cracking catalyst is separated with crackate.With the coke on the coking cracking catalyst and oxygen combustion to produce cracking catalyst.Crackate separates in main fractionating tower.At least a portion is compressed so that the top of compression materials flow to be provided from the overhead of main fractionating tower.With flow from the top of compression materials flow, separate and with at least a portion flow depropanizing so that the C of alkene and paraffinic hydrocarbons to be provided
4-C
7Materials flow.With C
4-C
7The materials flow of alkene and paraffinic hydrocarbons infeeds in the zone of transformation with C
4-C
7Conversion of olefines becomes more macromolecule C
4-C
7Derivative compound.
In one embodiment, the present invention relates to be used for become more high-molecular weight compounds with the equipment of preparation FCC charging conversion of olefines.This equipment comprises and being used for comprising rich C
3The overhead of overhead and rich C
5Bottom stream separation processes separation column.The alkylation reaction of arene device is communicated with the bottom line of technology separation column with rich C
5Alkene in the bottom stream is used alkylating aromatic hydrocarbon.The product tower be communicated with the alkylation reaction of arene device with alkylaromatic hydrocarbon from from rich C
5Separate in the unreacted compound of bottom stream.At last, the FCC reactor drum is communicated with the bottom line of product tower.
In another embodiment, the present invention relates to be used for become more large compound with the equipment of preparation FCC charging conversion of olefines.This equipment comprises and being used for comprising rich C
3The overhead of overhead and rich C
5Bottom stream separation processes separation column.First zone of transformation is communicated with the bottom line of technology separation column with C
5-C
7Conversion of olefines becomes more macromolecule C
5-C
7Derivative compound.Second zone of transformation is communicated with the overhead line of technology separation column with C
4Conversion of olefines becomes more macromolecule C
4Derivative compound.The product knockout tower is communicated with first zone of transformation with C
5-C
7Derivative compound never separates in the compound of reaction.At last, the FCC reactor drum is communicated with the bottom line of product knockout tower.
In yet another embodiment, the present invention relates to be used for the FCC conversion of olefines is become the more equipment of large compound.This equipment comprise be used to make cracking catalyst contact with the hydrocarbon incoming flow with hydrocarbon cracking is become to have the crackate hydrocarbon of lower molecular weight and make sedimentation of coke on cracking catalyst so that the fluid catalytic cracking reactor of coking cracking catalyst to be provided.Catalyst regenerator burns coke on the coking cracking catalyst and oxygen so that regenerated cracking catalyst.Main fractionating tower is communicated with to separate crackate with fluid catalytic cracking reactor.Compressor is communicated with the overhead line of main fractionating tower with the overhead of compression at least a portion from main fractionating tower.Receptor is communicated with so that flow is separated from the top of compression materials flow with compressor.The technology separation column is communicated with receptor with at least a portion flow depropanizing.Zone of transformation is communicated with the technology separation column with C
4-C
7Conversion of olefines becomes more macromolecule C
4-C
7Derivative compound.
The detailed Description Of The Invention that other features and advantages of the present invention are provided by this paper, accompanying drawing and claims are learned.
The accompanying drawing summary
Fig. 1 is the synoptic diagram of FCC apparatus and FCC product recovery zone.
Fig. 2 is the optional synoptic diagram of FCC apparatus and FCC product recovery zone.
Fig. 3 is another optional synoptic diagram of FCC apparatus and FCC product recovery zone.
Fig. 4 is the synoptic diagram of oligomeric zone of transformation.
Fig. 5 is the optional synoptic diagram of alkylating aromatic hydrocarbon zone of transformation.
Definition
Term " connection " means material and in operation, allows between listed assembly mobile.
Term " downstream connection " means at least a portion and flow into the object outflow that the material in the downstream connection object can be communicated with from its in operation.
Term " upper reaches connection " means at least a portion and can flow into the object of its connection in operation from the effusive material of upper reaches connection object.
Term " tower " means distillation tower or is used to separate the tower that one or more have the component of different volatility, and it can have at the reboiler of bottom and at the condensing surface at top.Only if point out in addition, the condensing surface that each tower is included in top of tower is with condensation and make reflux the go back to top of tower and send the bottom of tower at the reboiler of tower bottom with gasification and with a part of bottom stream back to of a part of overhead.Can be with the feeding preheating of tower.Top pressure is the pressure of tower exit overhead vapor.Bottom temp is the liquid bottom temperature out.Overhead line and bottom line refer to from the clean pipeline of tower to this tower in the backflow or the downstream of boiling again.
As used herein, the rich materials flow that term " rich component materials flow " means from separation vessel has the charging bigger concentration of component of score from container.
As used herein, the lean stream that term " poor component materials flow " means from separation vessel has the charging littler concentration of component of score from container.
Detailed Description Of The Invention
We find with alkene and from containing C
4Heavier product, preferred C
4-C
7The paraffinic hydrocarbons of the FCC product of product stream separate and make olefin recycle to main FCC reactor drum or the FCC reactor drum that separates in simple method.FCC product recovery zone can have single main fractionating tower and single gas device.The present invention includes reaction zone, therein conversion of olefines is become different chemical species, make them more easily separate with the inert paraffins hydrocarbon.But transform and isolating alkene derivatives then recycling return main FCC reactor drum or the FCC reactor drum that separates in.
Turn to Fig. 1 now, the similar similar assembly of numeral wherein, Fig. 1 illustrates refining a complete set of equipment 6, comprises FCC apparatus section 10 and product recovery zone 90 as the one of which.FCC apparatus section 10 comprises reactor drum 12 and catalyst regenerator 14.Process variable generally includes 400-600 ℃ cracking reaction temperature and 500-900 ℃ catalyst regeneration temperature.Cracking is all carried out under the absolute pressure below the 506kPa (72.5psia) with regeneration.
Fig. 1 shows typical FCC reactor drum 12, and the heavy hydrocarbon charge or the raw oil materials flow that infeed through divider 16 are contacted with the regeneration cracking catalyst that is got into by regenerated catalyst standpipe 18.This contact can be carried out extending upward to the narrow riser tube 20 of reaction vessel 22 bottoms.Contacting of charging and catalyzer through coming the gas fluidized of self-fluidized type pipeline 24.In embodiments, with hydrocarbon charging or oil gasization, when the two upwards was delivered in the reaction vessel 22 along with riser tube 20, the hydrocarbon charging was cracked into light molecular weight hydrocarbon product in the presence of catalyzer thereafter from the heat of catalyzer.Inevitable side reaction takes place in the riser tube 20, stay deposits of coke on catalyzer, this has reduced catalyst activity.Thereafter use cyclonic separator that cracking light hydrocarbon product is separated with the coking cracking catalyst, said cyclonic separator can comprise initial separator 26 and one or two 28 stages of cyclone in reaction vessel 22.The gaseous state crackate leaves in reaction vessel 22 to the pipeline 32 to be delivered in the downstream product recovery section 90 through product outlet 31.Spent catalyst or coking catalyst need be regenerated with further use.The coking cracking catalyst with fall into stripping stage 34 after the gaseous product hydrocarbon separates, steam is injected the there to remove any residual hydrocarbon steam through nozzle.After the stripping operation, coking catalyst is delivered in the catalyst regenerator 14 through spent catalyst vertical tube 36.Optional spent catalyst pipe 56 is delivered to spent catalyst the reactor riser 12 through the spent catalyst inlet from stripping stage 34 with the speed of regulating through valve.
Fig. 1 has described to be called the revivifier 14 of burner.Yet the revivifier of other type is suitable.In catalyst regenerator 14, the catalyzer that air distributor 38 is introduced with contact coking is passed through in the materials flow of oxygenous gas such as air.Coke burns so that regenerated catalyst and stack gas to be provided from pyrogenic catalyzer.Catalyst regeneration process adds the heat of real mass in the catalyzer, and the heat absorption cracking reaction of energy to take place in the compensatory reaction device riser tube 20 is provided.Catalyzer and air upwards flow along the burner riser tube that is positioned at catalyst regenerator 14 40 together, and after regeneration, at first discharge through separator 42 and separate.Leaving the regenerated catalyst of separator 42 and the other recovery of stack gas uses the first and second stage cyclonic separators 44,46 in the catalyst regenerator 14 to realize respectively.Distribute from cyclonic separator 44,46 through dipping tube with the isolating catalyzer of stack gas, the poorer stack gas that contains catalyzer is sequentially left cyclonic separator 44,46 relatively simultaneously, and in flue gas line 48, leaves regeneration container 14 through flue gas outlet 47.Regenerated catalyst is carried back in the riser tube 20 through regenerated catalyst standpipe 18.Because the coke burning, the stack gas steam that in pipeline 48, leaves at catalyst regenerator 14 tops contains CO, CO
2, N
2And H
2O, and a small amount of other species.Hot flue gases leaves revivifier 14 with further processing through flue gas outlet 47 in pipeline 48.
FCC product recovery zone 90 exports 31 downstream via pipeline 32 and product and is communicated with.In product recovery zone 90, the gaseous state FCC product in the pipeline 32 is sent into the bottom of FCC main fractionating tower 92.Main fractionating tower 92 also exports 31 downstream with product and is communicated with.Can the several fractions of FCC product be separated and from main fractionating tower, takes out, be included in the pipeline 93 from the heavy oil slurry of bottom, the heavy cycle oil materials flow in the pipeline 94, the light cycle oil that in pipeline 95, takes out from outlet 95a and the heavy naphtha materials flow of pipeline 96, taking out from outlet 96a.Can with in any or all pipeline 93-96 cooling and the pumped back main fractionating tower 92 with usually at place, higher position cooling main fractionating tower.Gasoline and gaseous state light hydrocarbon in overhead line 97, from main fractionating tower 92, reclaim and in getting into king-tower receptor 99 before condensation.King-tower receptor 99 exports 31 downstream with product and is communicated with.
With removing in the hopper of aqueous streams from receptor 99.In addition, the light naphthar materials flow of condensation is taken out in bottom line 101, and overhead is taken out in pipeline 102 simultaneously.The top of the nearly main fractionating tower 92 of part pipeline 101 backflow tiebacks is so main fractionating tower 92 is communicated with king-tower receptor 99 upper reaches.Overhead in the pipeline 102 contains the gaseous light hydrocarbon that might comprise rare ethylene stream.Materials flow in the pipeline 101 and 102 can get in the gas recovery section 120 of product recovery zone 90.
Compression light gaseous hydrocarbons materials flow in the pipeline 106 can compile with the materials flow in pipeline 107 and 108, cools off and is delivered in the high pressure receptor 110.Can be with sending in the king-tower receptor 99 from the aqueous streams of receptor 110.In the high pressure receptor, the compressed vapour stream in the overhead line 112 separates with the flow in the bottom line 124.With the lower end of sending into elementary absorption tower 114 in the pipeline 112 from the hydrocarbon gas materials flow at high pressure receptor 110 tops.In elementary absorption tower 114, the hydrocarbon gas materials flow contacts with the unstable gasoline of in bottom line 101, sending into 114 upper ends, elementary absorption tower from king-tower receptor 99, to carry out C
3+ with C
2Separation between the-hydrocarbon.This separation further improves through more than the feed points of bottom line 101, infeeding from the stable gasoline of pipeline 135.Elementary absorption tower 114 is communicated with the overhead line 102 of king-tower receptor and bottom line 101 downstream of king-tower receptor 99 via pipeline 106 and 112.The rich C of liquid in the pipeline 107
3+ bottom stream is before cooling in the return line 106.Can send into the lower end on second absorption tower 118 in the pipeline 116 from the elementary exhaust flow on elementary absorption tower 114.Second absorption tower is communicated with 114 downstream, elementary absorption tower.The recycle stream that in pipeline 121, is delivered to the light cycle oil of 118 upper ends, second absorption tower from pipeline 95 absorbs most of C
5+ material and number of C
3-C
4Material.Second absorption tower 118 is communicated with main fractionating tower 92 and 114 downstream, elementary absorption tower.More be rich in C from second absorption tower bottom in the bottom line 119
3The light cycle oil of+material returns in the main fractionating tower 92 via the pump circulation of pipeline 95.Main fractionating tower 92 is communicated with downstream, second absorption tower via bottom line 119.Comprise main C
2The top product on second absorption tower 118 of the dry gas of-hydrocarbon (wherein hydrogen sulfide, ammonia, oxycarbide and hydrogen are removed with second exhaust flow in pipeline 122) can further be processed. Absorption tower 114 and 118 does not all have condensing surface or reboiler, but can use the pump circulation cooling circuit.
To in pipeline 124, send in the stripping tower 126 from the liquid of high pressure receptor with fractionation.Stripping tower 126 is communicated with receptor 110 downstream via bottom line 124.Most of C
2-stripping tower 126 tops remove and via overhead line 108 return lines 106 in.On the one hand, will send in the technology separation column 130 via pipeline 128 from the liquid bottom materials flow of stripping tower 126.Stripping tower 126 does not have condensing surface, but accepts the cooling liqs charging in the pipeline 124.
It is desirable to C
4-C
7Alkene send into FCC reactor drum 12 or the FCC reactor drum (not shown) of separating in, with further generation light olefin.Yet the C of paraffinic hydrocarbons and alkene
4-C
7Materials flow is recycled to the foundation that can produce the inert paraffins hydrocarbon in the FCC reactor drum 12.As far as all carbon numbers in the naphtha range, it is difficult dividing defection with paraffinic hydrocarbons and alkene.The present invention proposes conversion of olefines is become heavier compound, so they can easily separate than light paraffins with unconverted.
In embodiments, can be with the C in the overhead line 132
3And/or C
4The mixture flow of alkene and paraffinic hydrocarbons is delivered in the LPG splitter column 140.LPG splitter column 140 is communicated with overhead line 132 downstream of technology separation column 130.Can further handle isolating C in the overhead line 142 of LPG splitter column 140
3The materials flow of alkene and paraffinic hydrocarbons is to reclaim propylene.C
4The bottom stream of alkene and paraffinic hydrocarbons can be separated in bottom line 144.
A part of stable gasoline in the bottom line 134 can be recycled to top, elementary absorption tower to improve C more than the ingress of pipeline 101 and 112 in pipeline 135
3+ recovery.In one embodiment, can fractionation in petroleum naphtha splitter column 150 from the clean bottom stream 136 of debutanizing tower.C
6+, C
7+ or more preferably C
8The materials flow of+heavy naphtha can be reclaimed with further processing and/or storage in bottom line 152.Comprise C
5, C
5-C
6Or more preferably C
5-C
7The overhead of alkene and paraffinic hydrocarbons and naphthenic hydrocarbon and aromatic hydrocarbons provides in pipeline 154.
In one embodiment, can be with comprising C
5-C
7The overhead 154 of alkene and paraffinic hydrocarbons infeeds to be communicated with also with bottom line 134 downstream of overhead line of petroleum naphtha splitter column 150 154 and technology separation column 130 and can comprise C
5-C
7In first zone of transformation 160 of zone of transformation.Any, some or all of C
5-C
7Alkene can change into more macromolecule C in first zone of transformation
5-C
7Derivative compound.The suitable reactions that can in first zone of transformation 160, carry out comprises oligomeric and alkylating aromatic hydrocarbon.Can comprise C
5-C
7First product of derived products leaves first zone of transformation in pipeline 162.
Can be with the C in the bottom line 144
4The bottom stream of alkene and paraffinic hydrocarbons is delivered in second zone of transformation 170 that is communicated with overhead line 132 downstream of bottom line of LPG splitter column 140 144 and technology separation column 130.Second zone of transformation can be C
4Zone of transformation.C
4Alkene can change into more macromolecule C in second zone of transformation
4Derivative compound.The suitable reactions that can in second zone of transformation 170, carry out comprises oligomeric and alkylating aromatic hydrocarbon.Can comprise C
4Second product of derived products leaves second zone of transformation in pipeline 172.Can carry out identical method or diverse ways in each first and second zone of transformation 160 and 170.In Fig. 1, the second conversion elute in conversion elute of first in the pipeline 162 and the pipeline 172 compiles and gets in the stabilizer tower 180.Two pipelines 162 and 172 can be distinguished or get into jointly in the stabilizer tower 180.In addition, the materials flow in the pipeline 172 can be cooled and separate, and in this case, steam can get in the tower 180 more than the liquid feeding that can get into or not get into pipeline 162.Stabilizer tower 180 can be communicated with first and second zone of transformation 160 and 170 downstream.
Can take out with three kinds of materials flow fractionation and from stabilizer tower 180.Comprise the C that can be recovered in the pipeline 182
3The top stream of-material gets in the gas device or sends in the fuel gas.Can be with the C in the pipeline 184
4Paraffinic hydrocarbons sides stream, and materials flow is reclaimed or further processing in the LPG processing section or in oligomerization zones, such as hereinafter explanation.Comprise heavier C in the pipeline 186
4And C
5-C
7The bottom stream of derivative compound can get in the product splitter column 190.
The product splitter column respectively with can be communicated with bottom line 186 downstream of stabilizer tower 180 for first and second zone of transformation 160 of oligomeric or alkylation reactor and 170.As selection, pipeline 162 can not get in the stabilizer tower 180, but walks around it to product splitter column 190, and in this case, pipeline 172 gets in the stabilizer tower independently.The product splitter column can provide two kinds of materials flows.Can be with comprising C in the pipeline 192
5-C
7The overhead of unconverted materials reclaims with further processing, and for example further processing in the petroleum naphtha hydrogenation treater to remove desulfuration, is sent in the gasoline pool or is used for alkylation zone as mentioned below.Comprise C in the pipeline 194 with higher molecular weight
4And C
5-C
7The part of derivative compound such as alkylaromatic hydrocarbon or oligopolymer or all bottom stream can be used as charging and are recycled in the FCC reactor drum 12.Fig. 1 is presented at the recycle stream that gets into along with the primary feed in the pipeline 16 in the pipeline 194, but it can get in the riser tube 20 in different positions.According to an aspect, FCC reactor drum 12 is communicated with bottom line 194 downstream of product splitter column 190.Bottom fraction in the pipeline 194 can be returned in FCC reactor drum 12 or the different FCC reactor drum with other cracking to improve the yield of light olefin.
Fig. 2 shows the optional embodiment of Fig. 1.Only show a zone of transformation 160 ' among Fig. 2.(represent by the reference number of ') with having apostrophe for the element that is equivalent among Fig. 2 but is different from the element among Fig. 1.Identical among other part of among Fig. 2 all and Fig. 1.
On the one hand, the liquid bottom materials flow (it comprises a part of liquid stream in the bottom line 124) from stripping tower 126 is admitted in the technology separation column 130 ' in the pipeline 128.Technology separation column 130 ' can be communicated with stripping tower 126 downstream via bottom line 128.Technology separation column 130 ' can comprise depropanizing tower, and it can be with the rich C in the pipeline 132
3Rich C in overhead and the pipeline 134 '
4And/or rich C
5Bottom stream is separated.The C that can comprise alkene and paraffinic hydrocarbons in the pipeline 132 ' from the overhead of technology separation column
3Product, and the bottom stream in the pipeline 134 ' comprises C
4, C
5, C
6And/or C
7, hereinafter referred to as comprise the C of alkene and paraffinic hydrocarbons
4-C
7Materials flow.Bottom stream in the pipeline 134 ' also can contain C
5+ naphthenic hydrocarbon and C
6+ aromatic hydrocarbons and than the heavy naphtha component.
A part of petroleum naphtha in the bottom line 134 ' can be recycled to top, elementary absorption tower (more than the inlet of pipeline 101 and 102) to improve C in pipeline 135
3+ the recovery.In one embodiment, can fractionation in petroleum naphtha splitter column 150 from the clean bottom stream 136 of depropanizing tower.C
5+, C
6+, C
7+ or preferred C
8The materials flow of+heavy naphtha is reclaimed with further processing and/or storage in bottom line 152.Comprise C
4, C
4-C
5, C
4-C
6Or more preferably C
4-C
7The overhead of alkene and paraffinic hydrocarbons and naphthenic hydrocarbon and aromatic hydrocarbons provides in pipeline 154 '.
In one embodiment, can overhead 154 ' be infeeded and be communicated with the bottom line 134 ' downstream of technology separation column 130 ' and can comprise C
4-C
7In first zone of transformation 160 ' of zone of transformation.Any, some or all of C
4-C
7Alkene can change into more macromolecule C in first zone of transformation
4-C
7Derivative compound.The suitable reactions that can in first zone of transformation 160 ', carry out can comprise oligomeric and alkylating aromatic hydrocarbon.Comprise C
4-C
7First product of derived products leaves first zone of transformation and gets in the stabilizer tower 180 in pipeline 162 ', and can be like processing among Fig. 1 with C
4-C
7Derived products is sent into middle FCC reactor drum.
Fig. 3 shows the optional embodiment of Fig. 1 and 2.Only show a zone of transformation 160 among Fig. 3 ".The element that is equivalent among Fig. 3 but is different from the element among Fig. 1 is with having two apostrophes (") reference number represent.Identical among other part of among Fig. 3 all and Fig. 1.
Can be with bottom line 144 ' ' in C
4The bottom stream of alkene and paraffinic hydrocarbons is delivered to and LPG splitter column 140 " bottom line 144 ", the overhead line 132 of technology separation column 130, the bottom line 134 of technology separation column 130 and the overhead line 154 of petroleum naphtha splitter column 150 " first zone of transformation 160 that is communicated with of downstream " in.Bottom line 144 " but engage top pipeline 154 " or get into first zone of transformation 160 individually " in.
First zone of transformation 160 " can comprise C
4-C
7Zone of transformation wherein can be with any, some or all of C
4-C
7Alkene changes into more macromolecule C in first zone of transformation
4-C
7Derivative compound.Can be at first zone of transformation 160 " in the suitable reactions of carrying out can comprise oligomeric and alkylating aromatic hydrocarbon.Can comprise C
4-C
7First product of derived products is at pipeline 162 " in leave first zone of transformation and get in the stabilizer tower 180, and can be like Fig. 1 processing with C
4-C
7Derived products is sent in the FCC reactor drum.
First and/or second zone of transformation can comprise illustrative oligomerization reactor 200 among Fig. 4.Oligomerization reactor 200 can with the bottom line 144,144 of the LPG splitter column 140 of Fig. 1 and 3 " downstream are communicated with.Identical or the oligomerization reactor 200 that separates can with the technology separation column of Fig. 1 and 2 130,130 ' bottom line 134,134 ' and/or overhead line 154, the 154 ' downstream of petroleum naphtha splitter column 150 be communicated with.In one embodiment; Pipeline 144,144 ", the diolefine in the bottoms in 154 or 154 ' can in pipeline 202, carry with at first in selective hydrogenation district 206 with the selective hydrogenation catalyst reaction do not make them be saturated to paraffinic hydrocarbons fully so that the diolefine selectivity is saturated.The operation process for selective hydrogenation conditions suitable for example be described in US 6,166,279 with US 6,075,173 in.This type condition comprises the alkene that makes liquid phase in the pipeline 202 and paraffin stream and from the hydrogen of pipeline 208 temperature, 689-3447kPa (g) pressure and the 0.5-10hr (100-500psig) at 20-200 ℃ (68-392 ℉)
-1Air speed under with the mol ratio of 0.5-5 mol of hydrogen/mole diolefine through comprising at least a catalyzer that is selected from the metal of nickel, palladium and platinum that is deposited on carrier such as the aluminum oxide.Can use two or more reaction zones, but only show one.Each reaction zone can 0-20 recycle stream: the ratio of fresh olefin feed stream uses to the recycle stream (not shown) of the reactor effluent of reactor inlet.The remaining diene content of this method depends on the strictness of operation, can be 1-100wppm.
Elute in the pipeline 210 (wherein diene concentration less than in the pipeline 202) from the selective hydrogenation device can with pipeline 212 in 0, selectivity properties-correcting agent in a kind of, the some or all of paraffinic diluent (can be a part of paraffin stream in the pipeline 184 of Fig. 1 or 2), pipeline 214 and the elute recycle stream in the pipeline 216 mix, in pipeline 218, infeed in the oligomerization reactor 200 then.In oligomerization reactor 200, from the C of pipeline 144
4Alkene, from the C of pipeline 154
5-C
7Alkene or from pipeline 154 ' or 154 " C
4-C
7Alkene and oligomerisation catalyst under oligomeric condition, contact with olefin oligomerization to produce heavier alkene.Oligomerization reactor is shown as downflow reactor, also can be suitable but go up flow reactor.
The condition of oligomerization process operation comprises makes the fixed bed of olefin liquid through catalyzer such as SPA or sulfonic acid ion exchange resin such as Amberlyst A-15, A-35, A-16, A-36, Dowex 50 etc.Can use the formation of several methods restriction higher oligomers.These comprise when using the SPA catalyzer; Paraffinic diluent in the pipeline 212 is added in the oligomerization reactor; When using resin catalyst, a part of oligomerization reactor effluent in the pipeline 216 is recycled in the oligomerization reactor 200 and with 0.1-3.0 weight % oxidation selectivity improving agent in pipeline 214, adds in the oligomerization reactor.It is not crucial avoiding heavy olefins to produce.Therefore, can save a kind of or all materials flows among the pipeline 212-216.
When using the SPA catalyzer, suitable preferred operations condition is different from those when using ion-exchange resin catalyst.Use the preferred temperature of SPA catalyzer operation to be 40-260 ℃, be more typically 75-230 ℃, and the preferred temperature of spent ion exchange resin catalyzer operation is 0-200 ℃, is more typically 40-150 ℃.The preferred pressure of using SPA catalyzer operation as 689-8274kPa (g) (100-1200psig); Be more typically 1379-6895kPa (g) (200-1000psig); And the preferred pressure of using ion exchange resin catalyzer operation as 345-3447kPa (g) (50-500psig), is more typically 1379-2413kPa (g) (200-350psig).These pressure can remain on the lower end of this scope, so do not need other compressor that pressure is increased to more than the required system pressure of selective hydrogenation treatment reactor 206.The performance such as olefin(e) centent and the type that depend on the oligomerization reactor charging use the preferred air speed scope of SPA catalyzer operation to be 0.5-5hr
-1, the operation of spent ion exchange resin catalyzer is 0.3-20hr
-1Other catalyzer can be suitable.
The oligomerization reactor product is taken out from oligomerization reactor 200 through elute pipeline 220.Part oligomerization reactor effluent can be recycled in the oligomerization reactor with the control thermal discharge through recirculation line 216.Second section oligomerization reactor product gets in the flash drum 226 through process pipeline 222, and unreacted steam flow and the flow that is rich in oligomerization product are provided therein.Unreacted vapor stream is left flash drum 226 with further processing in vapor line 228.A part of steam flow in the pipeline 228 can be recycled in the oligomerization reactor 200 through pipeline 230 later in condensation and compression.Rich oligomerization product stream in the pipeline 232 takes out from the bottom of flash drum 226.The purge stream that is used for from the unreacted steam flow of pipeline 228, removing paraffinic hydrocarbons in the pipeline 234 adds in the pipeline 232 so that pipeline 236 to be provided, and it becomes pipeline 162,162 ' or 172.
In another embodiment, first and/or second zone of transformation can be for like the illustrative alkylation reaction of arene device 300 of Fig. 5.Alkylation reaction of arene device 300 can with the bottom line 144,144 of the LPG splitter column 140 of Fig. 1 and 3 " downstream are communicated with.Identical or the alkylation reaction of arene device 300 that separates can with the technology separation column of Fig. 1 and 2 130,130 ' bottom line 134,134 ' and/or overhead line 154, the 154 ' downstream of petroleum naphtha splitter column 150 be communicated with.In one embodiment; Can be in pipeline 302 line of pipes 144,144 " or overhead line 154,154 ' in bottom stream in diolefine with at first in selective hydrogenation district 306 with the selective hydrogenation catalyst reaction do not make them be saturated to paraffinic hydrocarbons fully so that the diolefine selectivity is saturated.The conditions suitable of operation process for selective hydrogenation has been described about Fig. 4.Hydrogen gets into the reactor drum 306 from pipeline 308.
Alkylation reactor 300 is injected in the materials flow that comprises alkene and paraffinic hydrocarbons from selective hydrogenation device 306 in the pipeline 310.On the one hand, can use moisture eliminator (not shown) on pipeline 310 so that water is removed to the lower concentration that possibly influence catalyzer.Expect that also other protection bed is to remove catalyzer poison.Although transalkylation reaction also takes place in alkylation reactor 300, alkylated reaction is main.Alkylation reactor is shown as the last flow reactor with respect to aromatic streams, but downflow reactor also can be suitable.With injecting alkylation reactor 300 in several pipelines 312,314 and 316 that leading to a front space 322,324 and 326 before the materials flow of alkene and paraffinic hydrocarbons in the pipeline 310 is in getting into catalyst bed 332,334 and 336 respectively.Catalyst bed 332,334 and 336 contain alkylation catalyst with aromatic hydrocarbons and olefin alkylation to produce korenyl.Aromatic feed in the pipeline 340 stream is infeeded in the alkylation reactor 300, there its alkene and paraffinic hydrocarbons mixing from pipeline 316 in bed front space 326 is also got in the catalyst bed 336.Aromatic feed in the pipeline 340 stream can be communicated with Fig. 1,2 or 3 pipeline 192 downstream or part is later derived from the outside materials flow from the pyrolysis gasoline of steamed cracking unit in hydrotreatment from preferably at least.Expect other aromatic streams source.
Fresh alkene and the paraffinic hydrocarbons mixing from pipeline 314 in bed front space 324 of the elute of catalyst bed 336 also gets in the catalyst bed 334.Fresh alkene and the paraffinic hydrocarbons mixing from pipeline 312 in bed front space 322 of the elute of catalyst bed 334 also gets in the catalyst bed 332.A large amount of beds in the alkylation reactor 300 repeat this method.Although what show in the alkylation reactor 300 is three catalyst beds, more or less bed and other reactor drum can be suitable.The alkylation outflow thing of alkylation reactor 300 is carried in elute pipeline 342.Interchanger 344 can be cooled to ideal temperature with the elute in the pipeline 342.The materials flow of alkylation reactor elute can be through the decompression of process pressure controlled valve or through the pressurization of process pump, its two all demonstration.Carry the elute pipeline 342 of alkylate and unreacted paraffinic hydrocarbons to become pipeline 162,162 ', 162 " or 172.
Benzene is the most important representative of alkylatable aromatic substance so far, and it can be used as the alkylation matrix in the pipeline 340.Aromatic feed stream can comprise 5-99.9 mole % benzene.More generally, aromatic substance can be selected from benzene, naphthalene, anthracene, phenanthrene and substitutive derivative thereof.Find that but most important substituting group classification on the aromatic kernel of alkylaromatic is the list that contains 1-20 carbon atom-or many alkyl structures part.Other important substituting group is hydroxyl structure part and alkoxyl group structure division, and its alkyl also contains 1-20 carbon atom.
Multiple catalyzer can be used in an alkylation reaction zone.The preferred catalyst that is used for the present invention is a zeolite catalyst.Common and the refractory inorganic oxides binder combination use of catalyzer of the present invention.Preferred adhesive is aluminum oxide or silicon-dioxide.Suitable zeolite comprises zeolite beta, ZSM-5, PSH-3, MCM-22, MCM-36, MCM-49 and MCM-56.Zeolite beta is described in US 5,723, in 710.Preferred alkylation catalyst is UZM-8.Catalyzer with FAU structure is suitable.Zeolite is with the amount of at least 50 weight % of catalyzer, and more preferably the amount with at least 60 weight % of catalyzer exists.Yet,, possibly need much little zeolite concentration if zeolite is provided on the stratiform ball or on enhanced surface.
Carry out alkylating actual conditions and depend on used aromatic substance and alkene.Owing to be reflected at least and carry out under the Partial Liquid Phase condition, can adjust reaction pressure is liquid phase to keep alkene at least in part.The gas phase olefin charging also can be suitable.As far as higher olefins, reaction can be carried out under autogenous pressure.Pressure can change in 101-13172kPa (gauge pressure) wide region (1-1900psig).As a kind of practice, pressure is normally at 1379-6985kPa (gauge pressure) (200-1000psig) in the scope, but usually at 2069-4137kPa (gauge pressure) (300-600psig) in the scope.Be suitable for using C
4-C
7But the alkene of scope is 60-400 ℃ with the alkylating TR of alkylaromatic, and the most common TR is 90-250 ℃.Reactant is generally to be enough to obtain 0.2-50hr
-1, 0.5-10hr especially
-1The mass velocity of liquid hourly space velocity pass through alkylation zone.But the ratio of alkylaromatic and alkene should be 1:1 and up to 20:1, the ratio of 2.0-1.0 is preferred.
Do not further describe, believe that those skilled in the art can use previous description, integrated degree ground uses the present invention.Therefore, it only is illustrative that aforementioned preferred specific embodiments is interpreted as, and the rest part of limit publicity content never in any form.
In preamble, only if point out in addition, all temperature are with a ℃ description, and all parts and percentage ratio are by weight.
In previous description, those skilled in the art can easily confirm principal character of the present invention, and make various changes and modifications of the present invention so that it is suitable for various uses and condition with can not departing from its spirit and scope.
Claims (10)
1. conversion of olefines is become the more method of large compound, it comprises:
Make C
4Alkene and paraffinic hydrocarbons and C
5-C
7Alkene and paraffinic hydrocarbons get in the zone of transformation to pass through with aromatic hydrocarbons C
5-C
7Olefin alkylation and with C
4Conversion of olefines becomes more macromolecule C
4Derivative compound and with C
5-C
7Conversion of olefines becomes more macromolecule C
5-C
7Derivative compound;
With C
4Derivative compound and C
4Alkene separates with paraffinic hydrocarbons;
With C
5-C
7Derivative compound and C
5-C
7Alkene separates with paraffinic hydrocarbons; With
With C
4Derivative compound and C
5-C
7Derivative compound infeeds in the FCC reactor drum.
2. make said C according to the process of claim 1 wherein
4Alkene and paraffinic hydrocarbons and said C
5-C
7Alkene gets in the identical zone of transformation with paraffinic hydrocarbons.
3. make said C according to the process of claim 1 wherein
4Alkene and paraffinic hydrocarbons and said C
5-C
7Alkene gets in the different zone of transformation with paraffinic hydrocarbons.
4. according to the method for claim 3, wherein said C
4First zone of transformation that alkene and paraffinic hydrocarbons get into is an oligomerization zones.
5. according to the method for claim 3, wherein said C
4First zone of transformation that alkene and paraffinic hydrocarbons get into is the alkylating aromatic hydrocarbon district.
6. conversion of olefines is become the more method of large compound, it comprises makes C
5-C
7First materials flow of alkene and paraffinic hydrocarbons gets in first zone of transformation with C
5-C
7Conversion of olefines becomes more macromolecule C
5-C
7Derivative compound; Make C
4Second materials flow of alkene and paraffinic hydrocarbons gets in second zone of transformation with C
4Conversion of olefines becomes more macromolecule C
4Derivative compound is with C
4Derivative compound and C
4Alkene separates with paraffinic hydrocarbons; With C
5-C
7Derivative compound and C
5-C
7Alkene separates with paraffinic hydrocarbons, with C
4Derivative compound and C
5-C
7Derivative compound infeeds in the FCC reactor drum.
7. according to the method for claim 6, wherein said C
5-C
7First zone of transformation that the materials flow of alkene and paraffinic hydrocarbons gets into is selected from alkylating aromatic hydrocarbon district and the oligomerization zones one.
8. be used for conversion of olefines is become the equipment with preparation FCC charging of large compound more, it comprises: be used for comprising rich C
3The overhead of overhead and rich C
5Bottom stream separation processes separation column;
Be communicated with the bottom line of said technology separation column, be used for said rich C
5Alkene in the bottom stream is with the alkylation reaction of arene device of alkylating aromatic hydrocarbon;
Be communicated with said alkylation reaction of arene device, be used for alkylaromatic hydrocarbon and from said rich C
5The product tower of the unreacted compound separation of bottom stream; With
The FCC reactor drum that is communicated with the bottom line of said product tower.
9. according to Claim 8 equipment, it further comprises with the overhead line of said technology separation column and is communicated with, is used for comprising rich C
3The LPG overhead of overhead and rich C
4The isolating LPG splitter column of LPG bottom stream.
10. be used for conversion of olefines is become the equipment with preparation FCC charging of large compound more, it comprises: be used for comprising rich C
3The overhead of overhead and rich C
5Bottom stream separation processes separation column;
Be communicated with, be used for the bottom line of said technology separation column C
5-C
7Conversion of olefines becomes more macromolecule C
5-C
7First zone of transformation of derivative compound;
Be communicated with, be used for the overhead line of said technology separation column C
4Conversion of olefines becomes more macromolecule C
4Second zone of transformation of derivative compound;
Be communicated with, be used for said first zone of transformation C
5-C
7The product splitter column of derivative compound and unreacted compound separation; With
The FCC reactor drum that is communicated with the bottom line of said product splitter column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410148939.2A CN103951539B (en) | 2010-03-31 | 2011-03-29 | For improving the method and apparatus of olefin feed weight |
Applications Claiming Priority (5)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US12/751,658 | 2010-03-31 | ||
| US12/751,623 | 2010-03-31 | ||
| US12/751,658 US8128879B2 (en) | 2010-03-31 | 2010-03-31 | Apparatus for increasing weight of olefins |
| US12/751,623 US8471084B2 (en) | 2010-03-31 | 2010-03-31 | Process for increasing weight of olefins |
| PCT/US2011/030266 WO2011123413A2 (en) | 2010-03-31 | 2011-03-29 | Process and apparatus for increasing weight of olefins |
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| CN201410148939.2A Division CN103951539B (en) | 2010-03-31 | 2011-03-29 | For improving the method and apparatus of olefin feed weight |
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| CN201410148939.2A Active CN103951539B (en) | 2010-03-31 | 2011-03-29 | For improving the method and apparatus of olefin feed weight |
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| EP (1) | EP2552867A4 (en) |
| KR (1) | KR101474889B1 (en) |
| CN (2) | CN102811982B (en) |
| BR (1) | BR112012024022A2 (en) |
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| WO (1) | WO2011123413A2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1989009757A1 (en) * | 1988-04-11 | 1989-10-19 | Mobil Oil Corporation | Alkanes and alkenes conversion to high octane gasoline |
| WO2002000578A2 (en) * | 2000-06-23 | 2002-01-03 | Chevron U.S.A. Inc. | Conversion of refinery c5 paraffins into c4 and c6 paraffins |
| WO2003018519A1 (en) * | 2001-08-23 | 2003-03-06 | Chevron U.S.A. Inc. | Process for converting synthesis gas into hydrocarbonaceaous products |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5380425A (en) * | 1993-08-31 | 1995-01-10 | Mobil Oil Corporation | Over alkylation and catalytic cracking for benzene conversion |
| FR2837199B1 (en) * | 2002-03-15 | 2005-09-16 | Inst Francais Du Petrole | METHOD FOR CONVERTING INTO MULTIPLE STEPS A LOAD COMPRISING FOUR OLEFINS, FIVE ATOMS OF CARBON OR MORE, FOR PRODUCING PROPYLENE |
| US6995295B2 (en) * | 2002-09-23 | 2006-02-07 | Exxonmobil Chemical Patents Inc. | Alkylaromatics production |
| US6740788B1 (en) * | 2002-12-19 | 2004-05-25 | Uop Llc | Integrated process for aromatics production |
| FR2859994B1 (en) * | 2003-09-19 | 2005-10-28 | Inst Francais Du Petrole | PROCESS FOR THE DIRECT CONVERSION OF A CHARGE COMPRISING FOUR AND / OR FIVE ATOMIC CARBON OLEFINS FOR THE PRODUCTION OF PROPYLENE |
-
2011
- 2011-03-29 RU RU2012145344/04A patent/RU2525113C2/en active
- 2011-03-29 KR KR1020127027777A patent/KR101474889B1/en active IP Right Grant
- 2011-03-29 EP EP11763302.4A patent/EP2552867A4/en not_active Withdrawn
- 2011-03-29 WO PCT/US2011/030266 patent/WO2011123413A2/en active Application Filing
- 2011-03-29 CN CN201180015077.0A patent/CN102811982B/en active Active
- 2011-03-29 BR BR112012024022A patent/BR112012024022A2/en not_active IP Right Cessation
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1989009757A1 (en) * | 1988-04-11 | 1989-10-19 | Mobil Oil Corporation | Alkanes and alkenes conversion to high octane gasoline |
| WO2002000578A2 (en) * | 2000-06-23 | 2002-01-03 | Chevron U.S.A. Inc. | Conversion of refinery c5 paraffins into c4 and c6 paraffins |
| WO2003018519A1 (en) * | 2001-08-23 | 2003-03-06 | Chevron U.S.A. Inc. | Process for converting synthesis gas into hydrocarbonaceaous products |
| US20030045591A1 (en) * | 2001-08-23 | 2003-03-06 | O'rear Dennis J. | Process for converting synthesis gas into hydrocarbonaceous products |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103951539A (en) | 2014-07-30 |
| KR101474889B1 (en) | 2014-12-19 |
| WO2011123413A3 (en) | 2012-04-19 |
| CN102811982B (en) | 2014-10-08 |
| BR112012024022A2 (en) | 2016-08-30 |
| EP2552867A2 (en) | 2013-02-06 |
| RU2012145344A (en) | 2014-04-27 |
| RU2525113C2 (en) | 2014-08-10 |
| WO2011123413A2 (en) | 2011-10-06 |
| KR20130025384A (en) | 2013-03-11 |
| EP2552867A4 (en) | 2016-01-06 |
| CN103951539B (en) | 2016-02-24 |
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